GB2134803A - Centrifugal thin film evaporator - Google Patents
Centrifugal thin film evaporator Download PDFInfo
- Publication number
- GB2134803A GB2134803A GB08403451A GB8403451A GB2134803A GB 2134803 A GB2134803 A GB 2134803A GB 08403451 A GB08403451 A GB 08403451A GB 8403451 A GB8403451 A GB 8403451A GB 2134803 A GB2134803 A GB 2134803A
- Authority
- GB
- United Kingdom
- Prior art keywords
- cone
- liquid
- enclosure
- evaporated
- basin
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G33/00—Dewatering or demulsification of hydrocarbon oils
- C10G33/06—Dewatering or demulsification of hydrocarbon oils with mechanical means, e.g. by filtration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/22—Evaporating by bringing a thin layer of the liquid into contact with a heated surface
- B01D1/222—In rotating vessels; vessels with movable parts
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
- B01D19/0042—Degasification of liquids modifying the liquid flow
- B01D19/0052—Degasification of liquids modifying the liquid flow in rotating vessels, vessels containing movable parts or in which centrifugal movement is caused
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/30—Fractionating columns with movable parts or in which centrifugal movement is caused
Description
1
GB 2 134 803 A 1
SPECIFICATION
Device and installations for the distillation by thin layer evaporation particularly of hydrocarbons, and process for operating this 5 device
Background of the Invention
The present invention concerns an evaporation process in thin layers, especially applicable to the dehydratation of organic or mineral products, in 10 particular heavy crude petroleums. This process can also be used for the purification of thermosensitive products, for the degassing of petroleum products issuing from cracking, for the separation of very stable emulsions. 15 The invention also concerns devices or installations allowing the operating of this process.
Brief Description of the Prior Art
Scraped or non scraped falling film apparatus, 20 with axial or external condensation, are already known.
This apparatus does not allow, with reduced floor space, to obtain considerable outputs; exhaustion of the residue is only total for low 25 distillate yields. For high yields, either feed is reduced, or the first partially concentrated residue must be pumped and sent to the feed in order to undergo a second evaporation.
Rotor apparatus called "centrifugal" apparatus 30 are also known. This apparatus is the most often heated by means of electric resistances, which necessitates a constant circulation in product on its surface during the temperature conditioning phases. A single apparatus only allows 35 recirculation of the residue by interruption of feed or by mixing with the load.
Brief Description of the Invention
With respect to known apparatus, the operating of the process according to the invention allows a 40 considerable improvement of the yield.
In the process according to the invention for the evaporation of liquid in thin layers, process in which the thin layer is formed on one of the surface of a hollow cone pointed towards bottom 45 and open towards the top, in rotation about its vertical axis, in a substantially cylindrical enclosure, wherein the pointed part of the said cone is immersed in a reserve of liquid to be evaporated and a communication between the 50 external face of said pointed part of the cone and the internal face of this cone is established so that the thin layer subjected to evaporation is formed on the internal face and on the external face of the cone. A doubling of the evaporation surface is 55 obtained.
The invention also proposes a device for operating the processes comprising a sealed enclosure having a generally cylindrical shape, of vertical axis, and at least one hollow cone pointed 60 towards the bottom and open towards the top, driven in rotation about its axis, which is also that of the enclosure, the bottom of this enclosure providing a basin for a reserve of liquid to be evaporated wherein the pointed part of the said 65 cone, that is solid, is immersed in the liquid reserve filling the said basin up to a level maintained constant by appropriate means and wherein at least one communication channel opening below the said level, in the external face 70 of this pointed part, through crosses this latter and issues in the internal space of the cone, thus establishing the communication between an external face of the pointed part of the cone and the internal face of this cone, the evacuation 75 means of the vapors being provided in the upper part of the enclosure, whereas feed means of the liquid to be evaporated are provided in the bottom part of the enclosure.
Each communication channel presents a rising 80 path between its opening in the external face of the cone and its outlet towards the internal face, this path being furthermore oriented in such a way that, during rotation of the cone, the opening of the channel precedes the outlet of this channel in 85 the passage of this opening, then this outlet by any fixed radial plane.
The device is applied to the construction of a "flash" distillation or especially rectification installation, as will be shown hereinunder.
90 Description of the Invention
The characteristics and advantages of the invention will be better understood from the following description, given solely by way of example with reference to the annexed drawings 95 in which:
Figure 1 is a schematic view, in section, of an embodiment of the evaporation device according to the invention, comprising a single cone, and adapted, for example, to a "flash distillation", with 100 an isotherm enclosure;
Figure 2 is a section along line II—II of Figure 1;
Figure 3 is a schematic view of a flash distillation installation according to the invention comprising three cones identical to that of Figure 105 1, comprising an isotherm enclosure;
Figure 4 is a schematic view of a cracked distillation installation, with a lagged enclosure.
In the embodiment selected and represented in Figure 1, the device according to the invention 110 comprises in an enclosure 1 of a generally cylindrical shape, a hollow cone 2 open towards the top and engaged in rotation by means (not represented) about a shaft 3 having a vertical axis.
On its lower part, the enclosure 1 provides 115 about the pointed part 4 of the cone, that can be truncated and which is solid, a liquid receiving basin at the bottom of which leaves a drawing off channel 6.
Means, not represented here, are provided to 120 ensure in the basin 5, the maintenance of the liquid collected at a constant level H. A cover 7 sealingly closes at its upper part the enclosure 1, through crossed by shaft 3, due to a sealing bearing 8.
125 A feed pipe 10 in liquid to be evaporated issues into the basin 5 of the enclosure 1 toward the
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GB 2 134 803 A 2
bottom of said enclosure.
In the cover 7 opens a vapor evacuation pipe 11, issuing into condensation means (not represented).
5 Due to a good thermal insulation and pipes 15 through crossed by a thermal regulation liquid, the enclosure 1, closed by the cover 7 is maintained at a selected constant temperature.
According to one characteristic of the 10 invention, at least one communication channel 12 (three in the example as shown in Figure 2), provided slant-wise in the pointed part 4, contacts the external face of the cone with the internal part of it; this channel 12 opens into 13 on the external 15 face 2a of the cone above the level H in the basin 5 and rises according to a rectilinear or concave run in the solid lower part 4 of the cone to issue into 14 in the internal space of the cone, above point H, opposite the internal face 2b of the cone. 20 At its upper part, the wall of the cone is completed by a flange 17 radially directed towards the exterior. The rotation speed of the cone about its axis must be sufficient for the centrifugal force above level H to be greater than 25 the forces of gravity, of viscosity and of surface tension exerted on the liquid.
As to the sense of rotation, it is such that the liquid is, due to the orientation of channels 12, sucked inside these channels by this rotation 30 (Figure 2). With this aim, the low inlet 13 of the channel, passes by any fixed radial plane prior to the high outlet 14 of this same channel during rotation of the cone.
Under these conditions, two thin layers of liquid 35 are formed, one in contact with face 2a directly in contact with the liquid contained in the basin 5, the other in contact with face 2b, by rising on the liquid by means of each channel 12 immersed in this same basin. These faces can advantageously 40 be made rough, for example, by sand-blasting or comprise grooves.
The mixture to be treated, heated to flash temperature in 10, is brought in the basin 5 which is disposed at the point of the cone. When the 45 immersion of the point of the cone is sufficient, the rotation of the cone ensures the rise of the liquid and its spreading out in thin layers on the internal and external faces of the cone, where the evaporation occurs. The formation of thin layers 50 from this mixture which can be, for example, a heavy crude petroleum, instantaneously provokes, on the surfaces of the cone the evaporation without boiling of the constituents of the mixture for which the temperature and absolute pressure 55 conditions are united and maintained constant, in the evaporation enclosure 1, by appropriate means (not represented).
The vapors produced are condensed, continuously outside the evaporation enclosure by 60 appropriate means, and stocked in a collector or eliminated continuously, by pumping by channel 11.
The non-evaporated liquid phase is centrifugal along the length of the flange 17 of the open cone 65 2 on the internal surface of the thermostated enclosure, in the form of a radial sheet 18, and runs down to basin 5.
It is in order to conserve the required thermal balance that it is necessary to thermostat the 70 liquid-receiving enclosure at the flash temperature involved.
When the level of the liquid contained in the enclosure is at the maximum defined herein-below, said level is prevented from continuing to 75 rise by a continuous drawing off in 6. The flow-rate of the drawing-off is subject to tmeasurement of the liquid level H, which is obtained by measuring the loss of charge provoked by this liquid column. Measurement of the drawing-off 80 flow-rate is carried out, for example, by a tachymeter installed on the geared pump ensuring the maintenance of the level.
According to this operation of the process, the two faces of the cone are used and allow, on the 85 one hand, a considerable feed flow-rate for a minimum of space required, and, on the other hand, a recirculation at extremely high flow-rate of the liquid phase thus allowing a quasi-total exhaustion in a very short operation time. 90 The yield of the unit is automatically adjusted, at its optimal level by the digital system that directs the piloting of the geared pumps so as to establish the maximum flow-rate, i.e. always keeping slightly below stoppage flow-rate. 95 In one application of the process to the dehydration of heavy crude petroleum, containing 15% of water a material having the following characteristics is used:
cone having an angle of
60° at its apex
100
total height of the cone
245 mm
height of solid cone
40 mm
diameter of the 3 channels
13 6 mm
opening diameter
250 mm
thickness of the wall
2 mm
105
rotation speed
450 tr/mn enclosure maintained at 150°C with a pre-heating at 80—95°C of the treated mass.
In this example, the feed flow-rate was about 15 l/h.
110 The retention volume, maintained in the basin 5 was about 150 ml.
The cone was sunken about 40 mn in the liquid, a depth sufficient to produce the driving effect required.
115 it is interesting to note that the vapors issuing from the external face of the cone must, in order to be evacuated, cross through the radial sheet 18 that favorizes the gas-liquid separation with an enrichment of the residual liquid.
120 The device of Figure 1 can be the object of a variation.
Besides channels 12, communicating the
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GB 2 134 803 A 3
outside of the cone 2 with the inside space of the cone, is provided at least one slanted light, disposed, for example, below a channel 12, crossing through the solid pointed part 4 of the 5 cone with the same orientation conditions as channels 12 with respect to the sense of rotation of the cone for the low inlet 21 and the high outlet 22 of this light, above point H.
The drawn-off liquid in 21 is pumped by the 10 light 20 and brought onto the external face 2a of the cone.
It is thus possible to obtain a satisfactory operation of the device by lowering the level H of the liquid in the basin 5 to a lower level H' 15 contingent on the inlet-apertures 13 and 21 in channels 12 and lights 20 are below this level H' and also the centrifugal force exerted at the level of 22 on the liquid layer of the wall 2a is superior to the viscosity, gravity and surface tension forces. 20 In order to maintain the level constant between H and H\ ensuring a hydraulic protection, any suitable means may be used: syphon, control adjustment actuated, for example, by determination of the feed flow-rate and the 25 drawing-off flow-rate and action on the flow-rate of the feed and drawing-off pumps.
In the device according to the invention,
settling time of the treated water on the evaporation surface is increased, which is 30 equivalent to a multi-passage with its advantages.
Furthermore, the volume of the fed phase with respect to the volume circulating is low and thus the incidence on the cooling installation due to the expansion is reduced.
35 The gaseous phase by load is increased, while the energetic consumption is reduced.
It is, of course, possible to dispose on a single turning shaft of a single enclosure, several cone devices according to the invention in order to 40 constitute installations ensuring the greatest possible flow-rates, and thus allowing to avoid the realization, which is delicate, of large-size diameter cones, which require much space.
As shown in Figure 3, it is possible to 45 superimpose several cones, for example three, fed in parallel. The feed on the two faces of the cones is carried out with the use of a hollow shaft 30, from which leave towards the faces of the cones, channels 12 and lights 20, as previously described. 50 The recirculation of the liquid is carried out in a hollow shaft 103 by means of a pump 31, fed in 32 by a heated load, at a pressure such that the loss of charge due to the height of the liquid (length of the hollow part of the shaft) is 55 negligible.
The vapors produced are led by blast-pipes 11 a, 11 b, 11 c, at each stage of the cone, towards a condensor (not represented).
The cone device according to the invention can 60 also be used advantageously for cracking units in rectification and in exhaustion.
It involves replacing the hole, blister and valve plates or any other system of plates, by stages of turning cones (Figure 4) four in this example, but 65 there can, of course, be more.
The evaporation occurs on each face of the cone in this layer, the heat and material (liquid-gas) exchange occurs on the "mist" formed at the open periphery of the cone, between the moment where the liquid is ejected from the cone and the moment where it enters into contact with the wall of the enclosure 1, this wall being lagged. The vapors produced on the directly lower cone come into contact with the outside film of the upper cone by forming an exchange by licking, then will create a second exchange of the same nature with the above-mentioned mist.
The liquid recovered on the wall of the enclosure in droplets 32 after exchange with the gas is, for one part, recycled on this plate by the channel 34 (valve 41) and, for the other part, sent through pipe-line 33 to the base of the directly lower cone in order to be distributed two thin layers on the external and internal faces of the cone, through distributing channels and lights having tangential perforations and undergoes an evaporation corresponding to the new temperature and pressure conditions prevailing on the lower cone. An increasing concentration gradient, in the most volatile products thus exists between the foot and the head of the cracked distillation column thus created.
This concentration gradient is not however accompanied, as in classic real plate columns, by a loss of charge as important as in said column. Indeed, the loss of charge of the dry column is practically nil; the loss of charge is only created by the difference of vapor density of the different products present in the column. The height of the liquid that must overcome the vapors is itself also very reduced since it concerns a liquid "mist", the thickness of which is always small.
The vapors produced by the cone at the "head" of the column are totally condensed and are, according to the rate of reflux imposed by operating of the unit, due to a reflux divider 35, in part collected as distillate in head in 36, and for another part reinjected in 37 under the head cone.
The "foot" cone functions as a reboiler of the bottom of the column, as a simple exhaustion mono-cone (as described herein-above, the residue being evacuated in 40). This system allows either unbroken operation or operation in batch. Furthermore, channels 34 can be provided, adapted to ensure a recycling of the liquid phase (the rate of which is adjusted by valves 41) on each plate and thus to increase the quality of cracking.
The process according to the invention allows, furthermore, to carry out cracking under widely various pressures, while leading to clear advantages over the known processes operating under reduced pressure.
Of course, the present invention is in no way limited to the embodiments described and represented and it can be adapted to numerous variants available to the man skilled in the art, without departing from the scope and spirit of the invention.
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GB 2 134 803 A 4
Claims (10)
1. Evaporation process in thin layers, in which the thin layer to be evaporated is formed by centrifugation on one of the surfaces of a hollow 5 cone pointed towards the bottom and open towards the top, in rotation about its vertical axis, in a substantially cylindrical enclosure, wherein the pointed part of the said cone is immersed in a reserve of liquid to be evaporated and a 10 communication is established between the external part of the said pointed part of the cone and the internal face of this cone, so that the thin layer subjected to evaporation is formed on the internal face and on the external face of the cone. 15
2. Device for operating the process according to claim 1, comprising a sealed enclosure having a generally cylindrical shape, of vertical axis, and at least one hollow cone pointed towards the bottom and open towards the top, driven in rotation about 20 its axis, which is also that of the reserve of liquid to be evaporated, wherein the pointed part of the said cone, that is solid, is immersed in the liquid reserve filling the said basin up to a level maintained constant by appropriate means and 25 wherein at least one communication channel opening below the said level in the external face of this pointed part through crosses this latter and issues in the internal space of the cone, thus establishing the communication between the 30 external face of the pointed part of the cone and the internal face of this cone, the evacuation means of the vapors being provided in the upper part of the enclosure, whereas feed means of the liquid to be evaporated are provided in the bottom 35 part of the enclosure.
3. Device according to claim 2, wherein each communication channel presents a rising path between its opening in the external face of the cone and its outlet towards the internal face, this 40 path being furthermore oriented in such a way that, during rotation of the cone, the opening of the channel precedes the outlet of this channel in the passage of this opening, then this outlet by any fixed radial plane.
45
4. Device according to either of claims 2 and 3, wherein the three communication channels are provided in the pointed part of the cone.
5. Device according to any of claims 2 to 4, wherein at least one light is provided in the
50 pointed part of the cone that it crosses through in order to establish a communication between the zone of the external face of the cone located below the level of the liquid in the basin and a zone of that same external face, above the level. 55
6. Device according to any of claims 2 to 5, wherein the upper edge of the cone comprises a radial flange, directed towards the outside of the cone, in the direction of the wall of the enclosure.
7. Device according to any of claims 2 to 6, 60 wherein the faces of the cone present rugosities and/or grooves.
8. Evaporation installation comprising the device according to claims 2 to 5, for operating the process of claim 1, especially for the "flash"
65 distillation of petroleum products, wherein the wall of the enclosure and of the cover closing the enclosure are provided with heating means to maintain their temperature constant, means being furthermore provided for the alimentation of the 70 liquid to be evaporated at a determined temperature.
9. Installation according to claim 7, adapted to ensure the greatest possible flow-rate, wherein several cones are superimposed on a single shaft,
75 this hollow shaft comprising a bore from which leave the channels and, where necessary, the lights corresponding to each cone, means being provided for the feed under pressure of this bore in liquid to be evaporated, and vapor collection 80 means being provided in the wall of the enclosure above each cone.
10. Evaporation installation comprising the device according to claims 2 to 5, for operating the process according to claim 1, especially for the
85 distillation and/or rectification, wherein it comprises several cones superimposed on a single shaft, the pointed part of each cone being associated to a liquid receiving basin, surrounding in a sealed manner the said shaft, and the upper 90 edge of each cone, with the exception of the lower cone, being associated to recovery spouts disposed on the wall of the enclosure, channels connecting each spout associated to a cone to the basin of the lower cone, the basin of the upper 95 cone being itself fed by a liquid fraction issuing from a reflux separator placed at the head of the installation.
Printed for Her Majesty's Stationery Office by the Courier Press, Leamington Spa, 1984. Published by the Patent Office, 25 Southampton Buildings, London, WC2A 1AY, from which copies may be obtained.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR8302208A FR2540739A1 (en) | 1983-02-11 | 1983-02-11 | DEVICE AND FACILITIES FOR THIN-FILM EVAPORATION DISTILLATION, ESPECIALLY FOR HYDROCARBONS, AND METHOD OF IMPLEMENTING SAID DEVICE |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| GB8403451D0 GB8403451D0 (en) | 1984-03-14 |
| GB2134803A true GB2134803A (en) | 1984-08-22 |
| GB2134803B GB2134803B (en) | 1986-06-18 |
Family
ID=9285831
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB08403451A Expired GB2134803B (en) | 1983-02-11 | 1984-02-09 | Centrifugal thin film evaporator |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US4584064A (en) |
| JP (1) | JPS59196702A (en) |
| DE (1) | DE3404531A1 (en) |
| FR (1) | FR2540739A1 (en) |
| GB (1) | GB2134803B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0147215A2 (en) * | 1983-12-21 | 1985-07-03 | R. Goodwin International Ltd | Fluid/fluid separator |
| FR2581891A1 (en) * | 1985-05-14 | 1986-11-21 | Variot Gilles | Molecular distillation process and device for its use |
| GB2220368A (en) * | 1988-07-04 | 1990-01-10 | Netzsch Mastermix Ltd | Solvent recovery |
| US5254219A (en) * | 1991-03-12 | 1993-10-19 | Vaclav Feres | Film-type evaporator |
| US5425849A (en) * | 1991-04-11 | 1995-06-20 | Feres; Vaclav | Film-type evaporator |
| DE19632547C1 (en) * | 1996-08-13 | 1998-04-16 | Vaclav Feres | Multistage centrifugal rotary evaporator having two main evaporation surfaces |
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|---|---|---|---|---|
| BR8600564A (en) * | 1985-02-11 | 1986-10-21 | Falvourtech Pty Ltd | CONTRA-CURRENT CONTACT DEVICE OR DISTILLATION COLUMN, SYSTEM TO REDUCE THE ALCOHOLIC CONTENT OF A DRINK CONTAINING ALCOHOL, SYSTEM TO REDUCE THE ALCOHOLIC CONTENT OF WINE, SYSTEM FOR REMOVING AROMA AND / OR TASTE OF FRUIT JUICE, DE-DESULFURIZING A LIQUID AND PROCESS TO DISTILL, DISTILL BY FRACTIONATION OR REMOVE A SELECTED VOLATILE COMPONENT, OR COMPONENTS OF A LIQUID |
| NL1001006C2 (en) * | 1995-08-18 | 1997-02-20 | Biomass Technology Group B V | Method and device for the thermal treatment of non-gaseous material. |
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| US20020092762A1 (en) * | 2001-01-18 | 2002-07-18 | Zebuhr William H. | Distiller employing recirculant-flow filter flushing |
| US6689251B2 (en) | 2001-01-18 | 2004-02-10 | Ovation Products Corporation | Cycled-concentration distiller |
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| US1620163A (en) * | 1926-01-11 | 1927-03-08 | Frank A Milliff | Process of and apparatus for refining petroleum |
| US2443070A (en) * | 1946-06-27 | 1948-06-08 | Distillation Products Inc | Vacuum distillation process and apparatus |
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| GB986337A (en) * | 1963-01-02 | 1965-03-17 | Vitamins Ltd | Improvements in or relating to distillation apparatus |
| US3282798A (en) * | 1963-01-30 | 1966-11-01 | Baldwin Lima Hamilton Corp | Apparatus for compressing vapors in the distillation of a rotary conical film |
| US3412777A (en) * | 1966-07-13 | 1968-11-26 | Alfa Laval Ab | Frusto-conical film type evaporator |
| DE1619695A1 (en) * | 1967-02-21 | 1971-07-01 | Bayer Ag | Method and device for the thermal treatment of liquids |
| DE2409502B2 (en) * | 1974-02-28 | 1976-09-02 | Feres, Vaclav, Dipl.-Ing., 7500 Karlsruhe | THIN FILM EVAPORATOR |
| SU546357A1 (en) * | 1974-09-30 | 1977-02-15 | Предприятие П/Я М-5885 | Multisection rotary thin film machine |
| CH619150A5 (en) * | 1976-01-30 | 1980-09-15 | Vaclav Feres | |
| DD139994A1 (en) * | 1978-11-17 | 1980-02-06 | Heinz Viehweg | APPARATUS FOR REMOVING TOOTH FLUIDS OF ROTATING MOUNTING PARTS |
| DE2911214A1 (en) * | 1979-03-22 | 1980-10-02 | Hoechst Ag | RECTIFICATION APPARATUS |
-
1983
- 1983-02-11 FR FR8302208A patent/FR2540739A1/en active Granted
-
1984
- 1984-02-09 GB GB08403451A patent/GB2134803B/en not_active Expired
- 1984-02-09 DE DE19843404531 patent/DE3404531A1/en not_active Withdrawn
- 1984-02-10 JP JP59024231A patent/JPS59196702A/en active Pending
- 1984-02-10 US US06/578,952 patent/US4584064A/en not_active Expired - Fee Related
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0147215A2 (en) * | 1983-12-21 | 1985-07-03 | R. Goodwin International Ltd | Fluid/fluid separator |
| WO1985002782A1 (en) * | 1983-12-21 | 1985-07-04 | R Goodwin International Ltd. | Fluid/fluid separators |
| EP0147215A3 (en) * | 1983-12-21 | 1985-08-28 | R. Goodwin International Ltd | Fluid/fluid separator |
| FR2581891A1 (en) * | 1985-05-14 | 1986-11-21 | Variot Gilles | Molecular distillation process and device for its use |
| GB2220368A (en) * | 1988-07-04 | 1990-01-10 | Netzsch Mastermix Ltd | Solvent recovery |
| GB2220368B (en) * | 1988-07-04 | 1991-12-18 | Netzsch Mastermix Ltd | Solvent recovery |
| US5254219A (en) * | 1991-03-12 | 1993-10-19 | Vaclav Feres | Film-type evaporator |
| US5425849A (en) * | 1991-04-11 | 1995-06-20 | Feres; Vaclav | Film-type evaporator |
| DE19632547C1 (en) * | 1996-08-13 | 1998-04-16 | Vaclav Feres | Multistage centrifugal rotary evaporator having two main evaporation surfaces |
Also Published As
| Publication number | Publication date |
|---|---|
| GB8403451D0 (en) | 1984-03-14 |
| JPS59196702A (en) | 1984-11-08 |
| US4584064A (en) | 1986-04-22 |
| GB2134803B (en) | 1986-06-18 |
| DE3404531A1 (en) | 1984-08-16 |
| FR2540739A1 (en) | 1984-08-17 |
| FR2540739B1 (en) | 1985-04-26 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PCNP | Patent ceased through non-payment of renewal fee |